DE1545339A1 - Process for the conversion of hydrocarbons - Google Patents

Description

DR. R. KOENIQSBERQER · DIPL-PHYe. R. HOLZBAUER DR. F. ZUM8TEIN - DR. E. A88MANN ° ^ TELEPHONE: IS »Τβ and Μ1011 ι B MDNOHIN β ■ TELMRAM * "XUMFAT ' ., SJSuJBBTlU ··", PO * T * OHECKKO * m <: MONOHKN 011Β0

BANKKO 4TOl BANKHAU H. A IFHKUWIR

A 85 88 ',

Vr- Expl,

PHlLMPS PETROLEUa ΟΟΚΡΑΠΥ, Bartleeville, Oklshorm, USA Process eur conversion of hydrocarbons

The invention relates to the conversion of carbon dioxide. It relates to a process and a device for co-ordinated naphtha cracking, oil refining, olefin dehydrogenation, Hydrotreatment and aromatic extraction.

If the same applicant agrees to submit a procedure! the Dieproportionl · tion that Naphthaoraokung and Olefindehydrierung are combined in one process, be erseugt in Ithylen and butadiene! times the method of the present invention are verhültnleB $ aai £ cheap products of this reaction were combined and wxat Heretellung -from verhältnienäeeig expensive products processed.

After the fire, let * · aigUtb · likflti, lutailta, IWMol and • In HutaauejMzycaaaterlal int iMhth · au met

• §lllf / 1S41

BATH ORIGINAL

It is possible to use a high quality and carbon black base material
Benzene from heating or fuel oil, gasoline and butene-oil boiler
to obtain products from a butadiene and ethylene production process.

The inventive method for producing a stream with high flavor content, the Bioh for use as a soot sauce is suitable, consists in

crack a naphtha stream in a naphtha crack zone,

Propellant or heating oil from the outlet of this naphtha crack zone
remove and guide the remaining part into a separation zone

remove a Cj hydrocarbon stream from the separation zone and this C 1-4 hydrocarbon stream to a butadiene recovery zone respectively,

to remove a butadiene stream from the butadiene recovery zone,

a butene-isobutylene stream from the butadiene recovery stream remove and .the butene isobutylene atom in an isobutylene farm lead zone eu,

a current btiteahaltigen do the Xeotutyltnentfarming · zone to remove and butene-Stroa in a butenes tö lungs zone lead,

Remove the oil fraction from the list below «end the best to lead to a deodorant *

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the effluent from the dehydrogenation zone to the burn-off zone to lead',

to remove a gasoline stream au <3 of the Abtrermzone,

take a stream from the iBobutylene removal unit, which contains isobutylene removed in this unit,

the gasoline stream, which contains isobutylene and the oil fraction, in to run a hydrotreatment zone $

Y'asserstoff in the hydrotreating zone to conduct and- "the B-vnRx stream with hydrogen treat zn (Hydrobehendlung), v / ser obei the current isobutylene and ülfraktionen contains

the effluent from the hydrotreatment zone into a flavor extract tionezone su lead,

Aromatics from the aromatic extraction zone in a benzene separation zone respectively.

Benzene from the Bensolabtrennsone zv. remove,

a stream of heavy aromatics from the IJenzolabtrennzone eu remove,;

the fuels or _c HeijsÖl and Stron heavy aromatics untex ¹ Education "ines current high Arora & tengehalt to mix,

and paraffins as olefins from this aromatic extrusion zone to be returned to the Kaphthacrackzoiie in the cycle,

9098 8 5 / TB 4 1 BAD ORIGINAL ^v

A throat water to.l'f stream is cracked, and the effluent is separated to drive bsw. To produce heating oil, gasoline, butene, butadiene, propylon and ethylene. The butadiene and ethylene are obtained from ajLS products. The butene is dehydrated to produce more butadiene. The propylene is disproportionated to obtain additional amounts of ethylene and butene, the butene being sent to the dehydrogenation stage. Isobutylene removed from butene prior to dehydrogenation, gasoline and fuel oil are hydrotreated and the effluent is solvent extracted to remove aromatics while recycling the paraffins and olefins to the gray stage. The aromatic part is further separated in order to produce benzene and a current of high τό «maten which is mixed with the heating or fuel oil to produce a high quality soot output meter. The effluent from the butene dehydrogenation and the C ₂ fraction from the propylene disproportionation are returned to the separation sequence for the hydrocarbon crack effluent.

In the present case, the term "disproportionation" is intended to mean the conversion of a hydrocarbon into similar hydrocarbons with higher and lower numbers of carbon atoms per molecule. The method is particularly applicable to non-tertiary aliphatic olefins with 3 to 6 carbon atoms r per molecule. Non-tertiary aliphatic? Olefins means olefins that have no carbon chain branch on a double bonded carbon atom. In the

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Disproportionation of propylene will be approximately equimolar amounts formed on ethylene and butenes.

Suitable dioproportionation catalysts for practicing the invention include oxides, sulfides, and carbonyls of Molybdenum and tungsten which are applied to silica, aluminum oxide or silica-aluminum oxide as a carrier, or any other suitable sieve proportioning catalyst. You operating conditions, the eioh for the catalytic converter and the Beβohiokung are chosen.

Catalysts, conditions and the like for use in the Dehydrogenation steps for the production of diolefins from Olefinbesohiokungen are known and need not be discussed. So is for example a suitable hydration process in the U.S. Patent 2,866,790,

The conditions and catalysts for the hydrotreatment stages are similarly known. For example, the procedure described in "Hydrocarbon Processing and Petroleum Refiner ¹¹ , November 1962, Volume 41, Ir. 11, Pages 201-202" is suitable Catalysts include molybdenum sulfide, nickel sulfide, and the like, on alumina or clay.

Pig is shown in the drawing. 1 one sit of a unit

faeetee system door Haphthaorackung, Propyltndi «proportion! eruBg

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Butene dehydration, hydrotreatment and aromatic extraction, '

Pig, 2 is a one-unit system for naphtha cracking, propylene disproportionation, butene dehydrogenation, Hydrotreatment and aromatic extraction, which shows the separation facilities in detail.

Fig. 3 shows a combined into a unit system for Naphtha packaging, propylene disproportionation, butene dehydrogenation, hydrotreatment and aromatic extraction using a simplified separation system.

Pig. Fig. 4 shows in greater detail the hydrotreatment facilities and flavor extraction, which are suitable for use in Pig's system »1, Pig. 2 or Pig. 3 are suitable.

In the one in Pig. 1, a hydrocarbon suitable for cracking is introduced into the naphtha cracking reactor 11, and the descent passes through the line 13 into the separation unit 14 A (^ hydrocarbon stream through line 18 and a σ, hydrocarbon stream through line 19 were removed

The C4 stream from line 18 goes to a butadiene recovery unit 21 out of which a purified butadiene stream is removed through the line 22 and a butene-Isolmtylen-

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Containing current is removed through line 23 and reduced to iaobutylene removal The stream containing butene, from which isobutylene has been removed, is passed through the line

26 passed into the butene oil removal unit 27, from which a purified Butenetrome through line 28 into the butene dehydrogenation unit 29 is performed. The effluent from the line 29 is passed through the line 31 and returned to the separation unit 14

The Ca stream from line 19 is passed into the diaproportioning reactor 33. The disproportionation effluent is passed through the line 34 into the separation unit 36, from which a C ^ -olene stream is passed into the butene deoiling unit 27 through the line 37. The lighter fractions of the abstroine in line 34 are returned through line 38 for recirculation to the disproportionation reactor 33 = if desired, a separate stream of G ₂ hydrocarbons and lighter hydrocarbons can be removed from the separation unit 36 through line 41.

The gasoline stream in line 17, the isobutylene stream in the Line 42 and the boiler product from the butene deoiling unit

27 in line 43 are all going into the hydrotreatment unit 46 led. Hydrogen is supplied through line 47. The effluent is directed into the aromatics extraction unit 48 which the paraffinic and olefinic fractions are returned through line 49 to the iTaphtha cracking unit 11, while

909885/1541 BADORIQlNAt-,

rend the aromatic components are passed through line 51 into a benzene separation unit 52, from which benzene through the Line 53 is removed and a heavier, high aromatic fraction through line 54 to mix with Heia oil in the line 16 is removed to the carbon black starting material which is withdrawn through line 56.

In the system shown in Fig. 2, a naphtha flow is in the Naphtha cracker 61 is passed through line 62 and the effluent is passed to the heat recovery and quenching unit 63 through the Line 64 out. In the heat recovery and quenching section the effluent from the naphtha cracking furnace is quenched in waste heat boilers, and a two-stage cooling tower provides further cooling by directing vapors up through the tower, deesen lower part an oil cooling and its upper part a multiple water cooling forms. For further heat savings, then Generated steam in the waste heat boilers in the Crackofenal.gassyetem. Mn Heating oil condenses in the cooling tower and all by-pass flows are removed from the circulating cooling oil through line 65.

The abetroin from the cooling tower is compressed and sent to the butane removal plant 66 alB evaporation flow and two condensate flows. This is done by removing waste from the heat recovery and Ab8chreokteil 63 through the compressor 67 into the relaxation karamer 68 is performed, with the condensate to the butane removal facility 66 passed through line 69 and the

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compressed head atom in the compressor 71 and to the expansion chamber 72 out of which the condensate to the butane separation unit 66 through line 73 and the steam to butane separation unit 66 through line 74. One freed from butane Gasoline becomes alo by-product from the butane removal plant 66 through line 76 removed.

The overhead stream is further compressed in compressor 77 and passed through an amine treatment unit to remove COg and HpS. The effluent from the amine handler 78 is sent to a caustic alkali washing and drying unit 79 where the effluent from the amine unit is caustic to remove the last traces of acidic gases and then water washed to prevent caustic bases from being carried over . The effluent from the caustic waso unit and drying unit 79 is fed to the propane removal system 80. The butene and the heavier soil product from the propane separation plant 80 is fed through line 81 into the butadiene recovery and purification unit, the first stage being a furfural absorber 82. Butadiene is absorbed into the absorber 82, and the enriched furfural goes into the. Furfural stripper 83 »whereby furfural sun furfural absorber 82 is returned through line 84. The butadiene-rich stream goes through line 85 into the butadiene column 86. A high-purity butadiene stream is taken off overhead through line 87, and the bottom product, which contains butenes, is passed through line 88 into line 89, which feeds the butene oiler 90.

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The overhead fraction from the purfural absorber is divided into two Streams separated. A current is passed through the line 91 into a cold acidic isobutylene removal unit 92 performed while the other stream is passed through line 93 into butane extraction column 94, causing butanes to build up in the system by removing these secondary streams. The de-butane stream from the extraction column 94 is passed through the line 95 and recombined with the stream that is sent to the isobutylene removal unit 92. The de-oiled overhead fraction from the butene oiler 90 is in the 3utendehydrogenation reactor 96, and the waste stream is passed through line 97 and returned to the separation system for the effluent from the naphtha cracker 91.

Preferably the waste stream from the dehydrogenation reactor is quenched in a waste heat boiler and in one with a chimney equipped oil and water cooling tower similar to the system for heat recovery and deterring the effluents from the liaphtha cracking furnace deterred

The propane and the lighter fraction from the propane removal system 80 are compressed in the compressor 101 and fed into the primary acetylene removal reactor 102. This unit is operated under conditions of high selectivity and low conversion _{in order to remove the majority of O 2} - and Cj-acetylenes, piperidine and butadiene, without any noticeable loss of ethylene or propylene. Preferably this Damp! dried again,

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to remove water ₍ formed from oxygen compounds in the feed to the acetylenes removal reactor, and then passed to cooling pass 103. Cooling pass 103 is a series of chiller and recirculation cooled heat exchangers and a centrifugal expander, with appropriate auxiliary tanks, pumps A hydrogen-rich vapor and a methane-rich vapor are removed as by-products, and the steam from this stream is liquefied and sent to methane removal plant 104. Preferably, the overhead fraction from the methane removal plant is recirculated through the cooling flue to remove the sensible heat The bottom product freed from methane, especially ethane, ethylene, propane and propylene, is led through line 106 into ethane removal plant 107. The overhead fraction from ethane removal is created h out the line 10Θ in the secondary Acetylenentfernungsreaktor 109, which is driven at a high loading _t Uciwrudlung and low selectivity to bring the acetylene content to a low value. The effluent from the secondary acetylene removal reactor is fed to the ethylene fractionation column 111 and separated into an overhead ethylene stream and an ethanetromal of bottoms. The ethane stream is removed through line 112, while the ethylene stream is conducted through line 113 to a methane stripper 114, with high purity ethylene being removed through line 116. If there is sufficient demand for ethylene, the ethane formed can be cracked to generate more

809885/1541 BAD ORIGINAL,

gen to generate at ethylene * The overhead stream from the methane stripper 114 contains sufficient ethylene to _r v / iedertrennung to justify, and dinner stream becomes the suction part of the compressor 101 through the line 117 as shown recycled O

The bottoms from the ethane removal plant 107 is passed through line 121 to an ethane removal unit 122. This unit is operated at high conversion and low selectivity in order to lower the methylacetylene and propadiene concentration sufficiently to avoid damage to the dieproportionation catalyst. The effluent from the acetylene removal unit 122 is fed to the disproportionation reactor 123. The effluent from the reactor 123 is fed through the guide 124 to the propylene splitter 126. The overhead. fraction _t which contains ethylene and lighter fractions »is returned to the ether removal system 107 through the line 127. E.η Febenstron? mainly propylene and propane is passed through conduit iii ι ^ 28 i'.m circuit to the inlet of the reactor j The Bodenprodulct, propane and heavier components, v / -: - lo by ε Eat line 132 to 131 Propansntfez'niingsanü.age led, nni aas Bcänenvroäv ^ t & vn the propane removal plant IJI is üin? ^ d: *. i 7srX * 'V: u3''i'3T

sobucy-

.iiiCB .'.- SO t.-'-

BATH ORIGINAL

tylenpolymeren in the line 136, and the butene oil bottom product in the line 137, together with hydrogen from the line 139 "fed to the hydrotreater 138" The effluent from the hydrotreater 138 is led to the aromatic extraction unit 141, with the paraffins and olefins in a circuit for cracking through line 142 while the aromatics are conducted through line 143 to a benzene separation unit 144 where the benzene is separated overhead and a heavier, high aromatic hydrocarbon stream is withdrawn from the bottom through line 146 . The bottom product from the benzene separation unit 144 is combined with fuel oil in line 65 and mixed in order to produce a soot production starting material with the desired aromatic content, which is withdrawn through line 147.

In Pig's system. 3, the operation is quite similar to that in Pig. 2, but becomes a much simpler one Separation system used. A haphthastrora is in the naphtha » craoker 151 introduced through line 152, and the effluent is passed through line 154 for heat recovery and quenching 153. The heat recovery and Abächreek section 153 may be similar to the corresponding section 63 of Pig. Be 2. The effluent from the cooling tower is in the compressor 156 and compressor 157 compressed and in the Ehtspannungskämmer 158 led »with the condensate from the expansion chamber to the Shtspannungskaamer 159. The irtierkopf fraction

909885 / 154L ₁ "BAD OPGlNAl.

a caustic wash from the relaxation chamber 158 and drying unit 1.61 and the compressor 162 in the expansion chamber 163 led. The upper part of the head from the relaxation Chamber 143 is converted into a relaxation chamber through a heat exchange tube 164 166 led. The condensate from the chamber 166 is in the methane removal system 16? guided. The bottoms from methane removal 167 goes to the acetylene remover tion unit 168 and then sum of ethylene fractionation tower 169 ge leads, from which an ethylene product stream overhead and ethane

• *

ground away from the ground. The condensate from the expansion chamber 163 is passed through a removal unit 171 for CU acetylenes led into the product splitter 172. The overhead portion off the expansion chamber 159 also goes through the acetylene remover processing unit 171 in the product splitter 172, the overhead portion from the product splitter 172 is introduced into the stream containing the bottoms from the methane removal plant ^ 67 and through the acetylene removal unit 168 into the ethylene fractionation tower 169 led. An IT level trom is removed from the product splitter 172 and used for propylene disproportionation S " unit 173 out, wherein the product from the unit 173 to Product splitter 172 is returned,

The bottom product from the product splitter 172 is fed into the furfural absorber 173. The enriched furfural _t τ / hich contains butadiene, is passed into the Furfuralstripper 177, and the butadiene-containing stream is stripped from furfural and is guided in the Butadienkolonne 178th Butadiene goes overhead

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also removed from column 576, while the bottom product is fed to the furfural adorber ΐ 76. Uao raffinate nus the absorber 176 is fed into the xfjobutylon removal unit ¹ Yo * with isobutylene from it through dip. Line 179 is removed and the remaining Stron is passed to butene oiler 180. A make-up stream from line 131, which leads the raffinate from absorber 176 to isobutylene removal unit 178, is removed through butane extractor 182. Me butanes are removed as raffinate from the B extractor 182, while the butenes are recovered and returned to the line · 8ί. The overhead fraction from the butene de-oiler 180 is fed into the butene dehydrogenation unit 186, and a product stream is returned to the compressor 156.

A banking 'Instron in Leitvng! 8b Isobutylenstroin ir "line 179 and the bottom product auö the ^{Bivfcenentöler!} 80 in the line · 187 are fed into the Hydrobehandüer -9 ^ together with hydrogen from line 92.," The -Abetrom from the hydrotreater 19 * is sur Aromatenextraktionseinhei ¹ *; 193 * _s out with paraffin ^ ji; e. mid olefin to ITaplithe.craoker through line 194 siirüekgefüiir-t v / ?? e & s, while the aroma "by tenkonzentrat the Laitnng 196 led to an isolation unit 197 Trf.rd _t . The Bonrsol wi "? d vCoev head sas this! sisilieii removed j wa.hr« 5i! a? i "X ⁵ c: -n sttliwersmr livülssr ^^ seeustofiß ml'-high Aromatii'igehix ^ -l- before: 3adt? ri ZycgQi: iomn9" ii κ: 4: -: i "i * T?: o : ^! , u --- "br; 7 /.-. iieisöv from άΰΐ ' Loi.v -'. '. ng ^: GC vt;? ^ f., i. \ ji; mi κ ^ ΰ, β- ^ ΐΊ '"i: yfi, im ei ::

f. ? *> ο c - ■; · ■ ■■ ·· -

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-ID

It is evident that many elements of a complete technical system in the description of the specified embodiments of the invention have been omitted for better clarity and for the sake of brevity. In many cases special amendments can be applied. For example any suitable disproportionation catalyst can be used in the disproportionation reactor, any suitable butenedehyd Hydrogenation catalyst can be used in butene dehydrogenation reactor and any suitable hydrotreating catalyst can be used in hydrotreatment reactor. In a corresponding manner, separation steps such as fractional distillation, solvent extraction and the like can be used where they are suitable and can be replaced by a person skilled in the art. The invention is based on the combination and is therefore not based on a particular one Type of cracking, disproportionation, or dehydration Hydrotreatment reactor or special purification or separation stages limited. Many details τοη facilities that are in

' A technical system required have been omitted, including, for example, parts such as pumps, valves, control devices and the like.

Fig. 4 shows in more detail the hydrotreatment, aromatics extraction and aromatics separation of Flg. 2. gasoline from line 76, Isobutylene from line 136 and butene oil bottoms in " of line 137 are heated in a heater 201 and transferred to a first stage hydrotreater 202. fed in. Of the

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The effluent from the treatment room 202 is in one treatment unit of the second Stage 203 treats the effluent from the treator 203 is cooled in the condenser 204 and fed into the high-pressure separator 206. If desired, part of the flow from the handler 202 are passed in a secondary line. The gaseous overhead fraction from separator 206, which is water-- ' contains substance, depending on the desire or requirement in the cycle recycled or blown off while bottoms are transferred to stabilizer 208. The overhead product from stabilizer 208 is fuel oil, which is transported through line HO is removed while the bottoms is fed to the separator 20Π, from which a heavy flow through the line 148 is removed, with the overhead portion for Aromatex » traction 11-1 is performed, which the aromatics extractor 211 and comprises the stripper 212. The paraffin returned in the cycle and olefin stream is through line 142 and the aromatics « current to benzene separation unit 144 passed through line 143, The benzene outlet 145, the aromatic stream H6, the heating oil resp. Fuel oil stream 65 and the stream of deodorant soot starting material 1 * 7 are described above in connection with FIG.

The following example explains the invention without describing it * to restrict "

example

In an example of the implementation of the invention according to the Operation according to lig. 2 comprises the Beschiokungsstrom to Grackreaktor 61 is a wide range naphtha that consists of a

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Kuwait crude oil is made. DaB naphtha has a boiling range from 40 to 180 ⁰ C (105 to 352 ⁰ P), a density of 64.3 ° API and contains 72 vol. £ paraffin (44 # n ~ paraffin), 18 vol. # Naphtha and 10 vol . # Aromatics, and practically no olefins. The operating conditions of the various units of the system are given in Table I and the material balance in Table II. The numbers of these streams correspond to the numbers in Pig. 2.

Table I Operating Conditions

Naphthic crack furnace

Danp: 7 / KW ratio: 0.7

From Jaesdruok: 1.76 ata (25 peia)

Outlet: (? 1450 bia 1500 °) 788-816 ⁰ C heat recovery JND quenching

Steam generated at 22.1 ats (315 peia) _Λ KUhLturmeinlassi 1.4 * ata (20 peia) 26O ° O (50O ⁰ P) Kühlturmauelaee: 1.27 ata (18 peia), 40.5 ⁰ C (105 ⁰ F)

1. Korapreseor level _ _Λ

«1η1βββι1.25 ata (17.7 peia), 39 ⁰ C (10O ⁰ F) Auslaset37 ata (48 peia) 102 ⁰ C (215 ⁰ F)

, 5 (, p), 39 (Auslaset, 37 ata, (48 peia), 102 ⁰ C (215 ⁰ F) 2750 PS », 780 ■ * / ■! * (27,435 OFM)

1. Relaxation _Λ . 2.95 ata (42 psia), 15.6 ⁰ O (60 ⁰ F)

2. Coapressor stage; _Λ

Binlassi 2.95 ati (42 peia). 15.6 ⁰ C (6O ⁰ F) discharge 8.3 a? A (118 pel "), 86.7 ⁰ C (188 ⁰ F) 2350 PS *, 266 u '/ uln (7992 OFM) 2" relaxation. .

7.73 ata (110 paia), 15.6 ⁰ C (6O ⁰ F)

C-6 butane removal _ _Λ

RUokfluestrosmelt 7.03 ata (100 peia), 16.7 ⁰ C (62 ⁰ F) reboiler steami 7.73 ata (110 peia), 156 ⁰ O (313 ⁰ F)

* PS »US PS EU 74 ¹ J, 8 WatV

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Table I (continued)

3 * Compressor level _ _

Inlet 7.03 ata (100 psia), 16.7 C (62 ° F) Outlet: 17.9 ata (255 peia), 85 ⁰ C (185 ⁰ P) 2150 hp *, 98.5 m ⁵ / min (3479 CPIi )

Amine treatment t%, η

Absorbertunni 17.6 ata (250 psia), 71 C (160 ⁰ F) input,

57 ⁰ O (135 ⁰ P) output, 95 fi COg removal

Caustic washing and drying

Caustic tower: 17 ₉ 2 ata (245 psia), 57 ° C (135 ⁰ Pj _ water washing tower 17.6 ata (250 paia), 5 ^ ⁰ C _n (135 ⁰ P) Trookner inlet.t 16.2 ata (230 psia) , i {i _{ 6 "C (60" P)

Dryer outlet: 14.8 ata (210 psia), i5.6 ^u C (60 ^υ Ρ)

Propane removal _n

Reflux drum: H, "" ata (200 psia) - ". 8 ⁰ C (0 ^M P) reboiler bowl: 14.8 ata (210 psia), 94 ⁰ C (202 ⁰ P)

Reflux drum; 7.03 a.ta (100 pslaj, 59 ⁰ C (138 ⁰ P)

), 150.5 ⁰ C f? N ^ ^ö P)

Furfural absorber

Reflux flow rate

Reboiler steam! 8.44 ata (120psia

Purfural stripper _nn

Reflux drum: 4.57 ata (65 psia), 4.3 C (1ΚΓΡ) reboiler bowl: 5.62 ata (80 psia), 165 ⁽ C (329 ⁰ P)

Butadiene _{column nn}

Reflux drum: 5.27 ata (75 psia), 4D, 5 ° C (105 ^u F) reboiler bowl: 6.33 ata (90 peia), 71.7 ⁰ C (161 ⁰ P)

Butene oiler _nn

Overhead steam: 5.98 ata (85 psia), 58 ^O CM36 ° F) reboiler steam: 6.33 ata (90 peia), 85.5 ° C (186 ⁰ P)

Isobutylene removal

Standard extraction with cold sulfuric acid

Butene extraction column

Turbo head: 7.73 ata (110 psia). 38 ⁰ C MOO ⁰ P) _n tower floor: 10.5 ata (150 psia), 65.5 ⁰ C ( ^{150 0} P) extractant furfural

Butendehydrogenation reactor

Phillips R ~ H90 catalyst Reactor pressure 1.23 ata (17.5 paia) Inlet temperature: 7O5 ° C (130 * ^.?) Outlet temperature: 662 ° C (1223 PJ Steam / KW ^ ratio: 12

90988 5/15 41

Table I (continued)

4th compressor stage

Inlet: 13.95 ata (198 psia), 15.6 ⁰ O (6O ⁰ P) Outlet: 36.9 ata (525 psia), HO ⁰ C (230 ⁰ P) 1750 hp *, 36.6 mVmin (1292 CPM)

Primary Ethylene Removal Unit Girdler G-73 Catalyst

Reactor Conditions: 36.6 ata (520 psia), 177 ⁰ O (350 ⁰ P)

Cooling train

13 refrigerated and interchangeable units in series

97 hp * centrifugal expansion pumps

Inlet: 34.1 ata (485 psia). 13 ⁰ C _n (55 ⁰ P)

Discharge set 33.7 ata (480 psia), -12 ⁰ C (10 ⁰ P) 33.0 ata (470 peia), -64 ⁰ O (-84 ⁰ P) 32.8 ata (466 psia), -101 ⁰ O (-15O ⁰ P) _n

Hydrogen separator: 32.0 ata (455 psia) -129 0 (-200 ⁰ P)

Methane removal _ft

Return flow drum: 29.9 ata (425 psia), -97 ° C (-142 ⁰ P) reboiler steam: 30.6 ata (435 psia), 11 ⁰ O (52 ⁰ P)

Ethane removal _n

Reflux drum: 28.1 ata (400 p8ia), _ft -1p ° 0 / 1Π) ReboiXeraempf: 28.8 ata (410 peia) »64 0 (147 P)

Secondary aoetylene removal unit Girdler G ~ 58 «catalyst
Hg / OgHg ratio: 2.0

Reactor Conditions: 27.8 ata (395 psia), 177 ⁰ O (35O ⁰ P)

Ethylene fractionation column _n

Reflux drum: 20.4 ata (290 psia), ~ 32 ° 0 (-25 P) reboiler steam: 21.1 ata (300 peia), -16 ⁰ O (3 ⁰ P)

Methanatripper

Rüokflusstrommel: 21.1 ata (300 psia), ⁰ O -34 (-29 P) Reboilerdämpfe: 21.8 ata (310 peia) -27 ⁰ O (-17 ⁰ P)

Cj acetylene removal unit

Girdler G-55 catalyst
H ₂ / C ₃ H ₄ ratio: 2.0

Reactor conditions: 34.1 ata (485 peia), 177 ° C (350 ° *)

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123 propylene _{disproportionation unit Λ Λ}

Reactor Conditions x 32.3 ata (460 psia), 454 ⁰ C (850 ⁰ P)

126 Propylene splitter RÜokflusstromm " Reboiler steam * 30,

Return drum * 29.5 ata (420 peia), 45.5 C (114 P)

», 2 ate (430 pBia), 115 ⁰ C (239 ⁰ P)

131 Propanetripper _ _n

Backfluaatronimeli 18.6 ata (265 psia), 50.5 ⁰ O (123 P) reboiler steam: 19.3 ata (275 psia), 119 C (246 ° P)

138 Hydrotreatment Catalyst Reactor conditions

141 aromatic extraction unit 144 benzene separation unit

9G9835 / 1541

Table II

64 69 1 Material balance, 72a Current, 0 kß / hour, 290906 L7SI / S88606 288 0 538.4 46 0 No. 0 18551 Component 6 2 + 142 O 14th JJL. 81 0 81 84 hydrogen 48 13.6 0.5 1257 0 0 Carbon monoxide 5459 15th 0 5867 2.7 0 Carbon dioxide 112 83 10 120 0 methane 8572 41.3 11 8513 0 0 Acetylenes 2779 336 8th 2802 0 44.5 Ethylene 6992 54.4 62.5 6948 0 Ethine 622 42.6 32.2 1041.5 0 0 Propylene 110 145 238 283.5 0 71.7 propane 910 650 39 839 0 11.3 Isobutane 610 649 26.8 3579 0 350 Isobutene 1245 130 85 4410 0 1068 Butene-1 273 1088 401 587 2.7 4599 Butadiene 806 783 557 4393 133 5614 n-butane 434 14210 80.3 3101 15618 870 trans-butene-2 15804 0 592 254.5 0 6073 cis-butene-2 2825 433 O 4190 Gasoline 47900 18173 1371 15756 158 Heating oil 47890 0 44643 0 Total Hydrocarbons 47900 3952 23OIO Furfural water
I.
S.
Ω

87 88 89 91.

44 * 5

44.5 44.5

- 2.7 175.5 1.4 72 23.6 - 11.3 20.4 11.3 3.6 5382 1808 6.8 350 116 2.7 3770 1.4 1066 352 11.3 14th 136.5 4612 1522 5558 175v5 56 ; 8 _t 6 - - 807 266 1822 4722 4251 1403 3770 5428 419 138

158 264
11366 5411 5956 10795 H643

Cn CO CO CO

L7SL / S88606

Table II (continued) component

hydrogen

Carbon monoxide

Carbon dioxide

methane

Acetylenes

Ethylene

Propylene

propane

Isobutane

Isobutene

Butene-1

Butadiene

n-butane

trane-butene-2

cie-butene-2

C ₅ -2O5 ° C

petrol

Heating oil

Total
Hydrocarbons

23

106 108 112 113 116 1.17 121

124

127 128 132

23

5.9

345

1491

18.6

13.2

1375

136

253 12.2 12.2 14th 1.4 81.6 6.8 2.3 1238 11166 11017 65.3 10948 10803 4J55 2873 2866 2873 1 1 31 9788 51.7 65.3 96 3608 5 5 101 2.3 53 * 1.8 5 ¹ I. 6.4 242 0.5 160 4021 437 *

535 5273 3889

2.7

12.7 1.4

4.5

149 2975

6.4 8.2

12962 17651

2.3 2.3 1.8 1 ₉ 8

6.4 142

0.5

2943 1662

106

2511

6.4

7294

2487

464

1.4

10420

18595

7.7 4.1

256

1105

2.3

1.8

1.4 20.4 2.3 1.4

0.5 141.5 136.5

2935 1658

2913 1658

106

3407 21778 27465 13955 2995 10963 10805 158 13509 38454 7299 24957 6197 4839

cn

cn

CO CO CO

LVS L / 988606 component

Table II (continued)

76 137 136 139 140 148 145 H6 65 gasoline de-oiler- isobu-barrel- heating- sulfur- ben- heavy- boilers- ethylene- fuel (propellant) - rere zol re (propellant), product poly- gae aro- oil

meres maten

hydrogen 2.7 1.4 156 20th Carbon monoxide 20th Carbon dioxide 23 492 Uethane 0.5 492 Acetylenes 2.7 Ethylene 20.4 21.3 2.7 5.4 Ethane 58.5 2.4 Propylene 263 899.5 propane 1.4 Iaobut «it Ieobutene 2.7 Butene-1 133 Butadiene 15640 264.4 n-butane trane-butene-2 cis-butene-2 (No) * 205 ⁰ O +

147 142 Ru3s- zu- friauerrücksches gang- Naphmatelei- tha rial tetee Naphtha

(Heiaöl) Total

Hydrocarbons 15778 * c - 20 * »° G

4218 4196 7226

342 4196

2825

763.4 136 4218 4196 2825

ZuH punaene et zung: Bensol

heavy aromatics non-aromatics.

263 899.5 7157 8388 39512

7157 8388 39512

cn

cn

CjO CaJ CD

£ 8 are possibly changes and modifications possible within the scope of the invention, which the process and the apparatus for producing ethylene, butadiene, Benzene and a carbon black feedstock along with by-products from a hydrocarbon stream describes *

909885/1541

Claims (1)

Patent claims (W process for generating electricity with a high aromatic content, which is suitable for use as a carbon black starting material, characterized by the following levels: Cracking of a naphtha stream in a naphtha cracking zone; Removal of fuel or heating oil from the effluent of this naphthacraolc zone and directing the remaining portion into a separation zone; Removal of a C 1-4 hydrocarbon stream from the separation zone and passing the C 1-4 hydrocarbon streams to a butadiene recovery zone; Removing a butadiene atom from the butadiene recovery zone; Removal of a butene-isobutylene stream from the butadiene recovery stream and directing the butene-isobutylene stroma to an isobutylene removal zone; Distance united butene-containing stream from the Isobutylenentferaungszone and passing the butene-containing stream into a Butenentölungszone; in the deoiling zone removal of an oil fraction and passing the residue to a dehydration zone; 909885/1541 BATH ORIGINAL Directing the effluent from the dehydration zone into the separation zone; Removal of a benein stroma from the separation zone; Removing from the isobutylene removal unit a stream containing isobutylene removed in that unit; Carrying this gasoline fuel, the isobutylene and the oil fraction contains, in a hydrotreatment zone; Directing water into the hydrotreatment zone and hydrotreatment of gasoline turbulence, isobutylene and oil fractions contains; Passing the effluent from the hydrotreatment zone into an aromatic extraction zone; Passing the aromatics from the aromatics extraction zone into a benzene separation zone; Withdrawing benzene from the benzene separation zone; Removing a heavy aromatics stream from the benzene separation zone; Using the propellant or heating oils and the heavy aromatic streams to form a stream with a high aromatic content and Recirculation of the paraffins from the olefins from the aromatic extraction zone into the naphtha aok zone. 909885/1541 2 ο method naoh claim 1, characterized by Removing a C1 hydrocarbon stream from the separation zone and passing the C1 hydrocarbon stream to a propylene disproportionation zone; Separating the effluent from the disproportionation zone and recycling a stream therefrom which contains C * hydrocarbons, to the separation zone and passing a stream therefrom containing O. hydrocarbons to the butene de-oiling zone; and Removal of ethylene from the separation zone. 3. The method naoh claim 1 or 2, characterized by Removal of fuel or heating oil from the effluent of the naphtha paint zone and passing the remaining portion into a first butane removal zone; Separation of a light stream containing butene and lighter components and a gasoline stream containing heavier components contains, in the first butane removal zone j Introduction of a light stream from the butane removal zone in a propane removal zone ι Separation of a light stream containing propane and lighter fractions and a heavy stream containing butanes, butenes and Contains butadienes in the propane removal zone; Introduction of this heavy stream from the propane removal zone into a butadiene removal zone. 909885/1541 BAD ORlGlNAl Z ⁰ I L t e eersei